JP5367350B2 - Process oil, rubber extension oil - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a process oil that is produced so as to have a desired aniline point and a desired kinematic viscosity. <P>SOLUTION: The process oil is obtained by mixing a solvent-deasphalted asphalt obtained by solvent-deasphalting a vacuum distillation residual oil of a crude oil with a solvent-deasphalted oil obtained by the solvent-deasphalting and/or a solvent extracted oil obtained by extracting the solvent-deasphalted oil with a solvent so as to have a desired aniline point and a desired kinematic viscosity. The process oil comprises 1.0-20 wt.% of the solvent-deasphalted asphalt and has the aniline point of 75-90&deg;C and the kinematic viscosity of 40-90 mm<SP>2</SP>/s. <P>COPYRIGHT: (C)2010,JPO&amp;INPIT

Description

  The present invention relates to a process oil and a rubber extending oil which are added to natural rubber and synthetic rubber to form a rubber composition.

  A rubber material applied to an automobile tire or the like is generally blended with mineral oil from the viewpoint of softening and improving processability. This mineral oil is called rubber lubricating oil or rubber compounding oil. Generally, rubber compounding oil is classified into rubber extending oil and process oil.

  The rubber extender oil is blended for the purpose of volume increase and plasticization by mixing with latex as an emulsified oil and co-coagulating it during the production of the extender rubber. On the other hand, process oil is blended for the purpose of facilitating mastication, additive blending, extrusion, Banbury mixer work, etc. by blending process oil into a rubber raw material that is difficult to knead in the rubber production process. . The process oil enters between the rubber polymers and acts as a lubricant to increase intermolecular fluidity. That is, intermolecular internal friction is reduced to impart plasticity.

  In particular, as the process oil, as described above, from the viewpoint of improving the plasticity of the rubber and reducing the hardness of the vulcanized rubber to improve the workability, the paraffinic, naphthenic, or aromatic hydrocarbon is used in accordance with the rubber type. Extracts containing many components are used. In addition to rubber materials such as natural rubber and synthetic rubber, these rubber extension oils and process oils are used as plasticizers for thermoplastic resins, constituents for printing ink, softeners for recycled asphalt, and the like.

  These rubber extender oils and process oils have a high aroma content extract as a by-product in the production of solvent refined oils by solvent extraction of the debris oil that has been removed from the vacuum distillation residue of crude oil. Many have been used.

  For example, Patent Document 1 proposes a process oil obtained by mixing an extract and a lubricating base oil having a polycyclic aromatic hydrocarbon (PCA) content of less than 3% by mass. In this process oil, various properties such as viscosity and aniline point are defined.

  Similarly, Patent Document 2 proposes a process oil characterized in that it uses various kinds of properties such as viscosity and aniline point, using as a raw material a degreased oil obtained by degassing a crude oil distillation residue. Yes. The process oil disclosed in Patent Document 2 is produced by mixing a predetermined mass% of an extract obtained by solvent extraction of the deoiled oil.

For example, as shown in Patent Document 3, a rubber softener obtained by mixing an extract and solvent-peeling oil has been proposed. In the technique disclosed in Patent Document 3, the property is indicated as having a viscosity of 35 to 55 mm ² / s at 100 ° C., but no other aniline point is mentioned.

  Patent Document 4 discloses an asphalt binder that is not used as a process oil for rubber, but contains asphalt: 0.5 to 20.0% by mass, and the balance is petroleum solvent extracted oil. . Examples of the asphalt used here include solvent deasphalted asphalt. Incidentally, in this patent document 4, since the use as process oil for rubber | gum is not assumed especially, the reference regarding various properties, such as a viscosity and an aniline point, is not made | formed.

In addition, as process oil mentioned about the property regarding a viscosity or an aniline point, it is disclosed also in patent documents 5-7, for example.
JP 2007-84675 A JP 2006-335833 A JP 2006-291195 A JP 2008-56742 A JP 2003-96244 A JP 2008-31211 A JP 2000-80208 A

  By the way, the above-described conventional rubber extending oil and process oil are both manufactured through a certain manufacturing process. For this reason, the viscosity and aniline point of the obtained rubber extension oil and the like are limited to specific properties, and in some processes, if the kinematic viscosity is determined, the aniline point is usually specified accordingly.

  However, in the case where it is assumed that the rubber material is applied to a tire for an automobile, etc., a certain aniline point for a certain kinematic viscosity is uniquely determined. The nature of the product itself is converged to a certain level, and various needs in the tire manufacturing process, for example, from the viewpoint of preventing the occurrence of so-called oil bleed, in which oil oozes out on the surface of the rubber compound, There are problems in that it is not possible to meet various demands such as ensuring the dimensional stability during compound molding, ensuring the elongation of rubber / compound, and obtaining desired rubber / compound viscosity and elastic modulus. It was.

  For this reason, so that the kinematic viscosity and the aniline point can be arbitrarily selected, in other words, one specific aniline point is not determined for one kinematic viscosity, but also for one kinematic viscosity. Conventionally, rubber extending oils and process oils that can freely select any arbitrary aniline point or can freely select any arbitrary kinematic viscosity for one aniline point have been desired. If rubber extension oil and process oil can be manufactured after freely selecting the combination of kinematic viscosity and aniline point, prevention of oil bleed as described above, ensuring dimensional stability during rubber / compound molding, rubber compound This is because it is possible to solve problems such as securing the elongation of the rubber, securing the predetermined rubber compound viscosity, and elastic modulus.

  In particular, in the past, in order to optimally adjust the kinematic viscosity and the aniline point, the adjustment of the ratio of the materials to be mixed was repeated several times through trial and error until reaching the desired kinematic viscosity and the aniline point. It had to take a lot of labor and time. Especially when producing 100t and 200t level process oils, it is necessary to change the process operating conditions at the plant level and determine whether or not the desired kinematic viscosity and aniline point have been reached without trial production. I could not. For this reason, every time a process oil consisting of a new kinematic viscosity and an aniline point is produced, it is necessary to remodel or install a plant, resulting in an increase in cost (time, energy, material consumption). .

  Therefore, the present invention has been devised to solve the above-described problems, and the object of the present invention is to produce a desired aniline point and a desired kinematic viscosity at low cost and with low labor. Is to provide a processed process oil, rubber extension oil.

Process oil according to the present invention, in order to solve the above problems, a solvent with respect to the asphalt, solvent deasphalted oil及beauty above Symbol solvent deasphalted oil obtained by solvent deasphalting the vacuum residue oil in oil Only the solvent-extracted oil obtained by extraction is mixed so as to have a desired aniline point and a desired kinematic viscosity.

At this time, the asphalt may be a solvent deasphalted asphalt obtained by desolvating the residual residual oil of crude oil. Further, the solvent deasphalted asphalt, is contained 1.0 to 20 wt%, the balance may be characterized in that it consists of only the solvent deasphalted oil及beauty above Symbol solvent extracted oil.

The aniline point may be 75 to 90 ° C., and the kinematic viscosity may be 40 to 90 mm ² / s.

  The rubber extension oil according to the present invention is characterized by comprising the process oil according to any one of claims 1 to 3 in order to solve the above-described problems.

According to the present invention having the structure described above, relative to the asphalt, solvent deasphalted oil及beauty Solvent extracted oil only by is formed by mixing the desired aniline point and the desired process oil such that the kinematic viscosity It becomes possible to obtain rubber extension oil. That is, it becomes possible to obtain a process oil and a rubber extension oil produced by freely selecting a combination of kinematic viscosity and aniline point. In particular, in the past, in order to optimally adjust the kinematic viscosity and the aniline point, the adjustment of the ratio of the materials to be mixed was repeated several times through trial and error until reaching the desired kinematic viscosity and the aniline point. However, according to the present invention, the kinematic viscosity and the aniline point with respect to the mixing ratio of only the solvent removal solvent and the solvent extraction oil with respect to the asphalt investigated in advance are required. Since the mixing ratio can be determined based on this, it is not necessary to remodel or install a plant each time a process oil having a new kinematic viscosity and an aniline point is produced as before, thereby reducing labor and cost. It becomes possible.

  Hereinafter, as the best mode for carrying out the present invention, a process oil and a rubber extending oil which are added to natural rubber and synthetic rubber to form a rubber composition will be described in detail.

  The present inventor has conducted extensive experimental research to solve the above-described problems and to produce a process oil so as to achieve a desired aniline point and a desired kinematic viscosity. As a result, the present inventor obtained a solvent-depleted oil obtained by removing the solvent from the solvent-removed asphalt obtained by removing the solvent from the vacuum distillation residue of the crude oil and / or the solvent-removed oil. It was found that the aniline point and the kinematic viscosity can be independently controlled to desired values by mixing the solvent extracted oil obtained by solvent extraction of.

  That is, the process oil to which the present invention is applied is obtained by mixing solvent deasphalted oil and / or solvent extracted oil with solvent deasphalted asphalt so as to have a desired aniline point and a desired kinematic viscosity.

  The solvent deasphalted asphalt is a so-called propane deasphalted asphalt obtained by using a propane or a mixture of propane and butane as a solvent with respect to the vacuum distillation residual oil. In the following description, solvent-deasphalted asphalt is described as an example, but the present invention is not limited to this. As an alternative to this solvent-desorbed asphalt, for example, straight asphalt, blown asphalt, etc. Any asphalt may be used.

Solvent deasphalted asphalt corresponds to a residue obtained by extracting solvent degreased oil (high viscosity lubricating oil fraction) from vacuum distillation residual oil. This solvent deasphalted asphalt is added mainly to adjust the kinematic viscosity, but is also used to adjust the aniline point. This solvent deasphalted asphalt has a penetration of 3 to 20 (1/10 mm) at 25 ° C., a softening point of 56 to 70 ° C., and a density of 1020 to 1065 kg / m ³ at 15 ° C. under JIS K2207. The properties shown in FIG. 2 can be obtained by setting the penetration of the solvent-peeling asphalt to 4 to 12 and the softening point to 68 to 60 ° C.

  In addition, about this solvent deasphalted asphalt, it is not limited to the range of the physical property mentioned above, What kind of range may be sufficient. However, the penetration and softening point correspond approximately one-to-one, and it is desirable to perform within the above-mentioned range in order to perform the adjustment described later more optimally.

Solvent debris oil is a debris oil after removing the above-mentioned solvent deasphalted asphalt by using propane or a mixture of propane and butane as a solvent to the vacuum distillation residual oil and performing debris treatment. is there. This solvent-peeling oil is added mainly to adjust the aniline point, but slightly contributes to the adjustment of kinematic viscosity. The kinematic viscosity at 100 ° C. of this solvent-peeling oil is 25 to 42 mm ² / s, and the density at 15 ° C. is 910 to 940 kg / m ³ . The properties shown in FIG. 2 can be obtained by setting the kinematic viscosity at 100 ° C. of the solvent removal solvent to 31 to 35 mm ² / s and the density to 920 to 935 kg / m ³ .

The solvent extraction oil is a so-called extract obtained by solvent extraction of solvent-peeled oil using a polar solvent. This solvent-extracted oil is added mainly to adjust the aniline point, but slightly contributes to the adjustment of kinematic viscosity. The kinematic viscosity at 100 ° C. of the solvent-extracted oil is 50 to 200 mm ² / s, and the density at 15 ° C. is 960 to 990 kg / m ³ . The property of FIG. 2 can be obtained by setting the kinematic viscosity at 100 ° C. of the solvent-extracted oil in the range of 60 to 70 mm ² / s and the density to 970 to 980 kg / m ³ .

  In addition, solvent deasphalting oil and solvent extraction oil are not limited to the above-described physical property ranges, and may be any range.

  In the process oil to which the present invention is applied, the aniline point that is the target of property adjustment means the minimum temperature at which the above-described process oil exists as a uniform solution with an equal volume of aniline. More specifically, this aniline point is expressed by the temperature when the process oil is mixed with an equal volume of aniline and cooled, and when the process oils cannot dissolve each other and become turbid, the aniline point is expressed in JIS K 2256. Details are defined. That is, the aniline point is an index indicating the affinity of the rubber mixed with the process oil, and is an index for determining whether to swell or dissolve mainly after blending the process oil and the rubber. Generally, the optimum value of this aniline point varies depending on the rubber type to be blended. For example, when blending natural rubber and process oil, the optimum aniline point of the process oil is 95 to 100 ° C. The reason is that if the aniline point is less than 95 ° C., it will swell after compounding with the rubber, and if the aniline point exceeds 100 ° C., the compatibility with the rubber will deteriorate, and the process oil will adhere to the rubber surface. There is a possibility of bleeding.

The kinematic viscosity is expressed as a proportional coefficient between a flow velocity gradient and a shear stress generated with respect to the velocity gradient divided by a fluid density. The kinematic viscosity, when applied as a rubber extending oil, is determined from the viscosity and elastic modulus of the target rubber and process oil compound. The kinematic viscosity may be configured in any range, but is generally preferably 40 to 90 mm ² / s when considering application of the process oil as a rubber extending oil for tire use. . If the kinematic viscosity of the process oil is lower than the required value (for example, 40 mm ² / s), the normal physical properties of the rubber to be blended will decrease, and if the kinematic viscosity is higher than the required value (for example, 90 mm ² / s) In addition, the viscosity and elastic modulus are too high, causing molding defects during blending, and consequently adversely affecting rubber properties.

  Next, the process oil manufacturing method to which the present invention is applied will be described in detail with reference to the flowchart of FIG.

  First, atmospheric distillation is performed on crude oil in step S11. The atmospheric distillation may be performed by any known atmospheric distillation apparatus and distillation conditions. For example, a crude oil composed of paraffinic crude oil, naphthenic crude oil or the like to be refined is heated to about 350 ° C. (temperature less than 360 ° C., which is a temperature at which hydrocarbon decomposition starts) in a heating furnace or the like. It is sent to a pressure distillation column, converted into petroleum vapor inside the atmospheric distillation column, and after cooling, is separated in order from a low boiling point to a high boiling point.

  Next, the process proceeds to step S12, and the atmospheric distillation residue obtained by atmospheric distillation in step S11 is distilled under reduced pressure. This vacuum distillation may be performed by any known vacuum distillation apparatus and distillation conditions. Through this vacuum distillation, the oil is separated and removed into vacuum gas oil, vacuum spilled oil, and vacuum distillation residue. In the present invention, only the vacuum distillation residue is used in future processes.

Next, the process proceeds to step S13, and the solvent is removed from the vacuum distillation residue obtained in step S12. Specifically, propane or a mixture of propane and butane is used as a solvent for the vacuum distillation residual oil, and the oil and asphalt components are separated. This oil component corresponds to the above-described solvent deasphalting oil, and the asphalt component corresponds to the above-described solvent deasphalting asphalt. Incidentally, in the step S13, the propane can be removed by mixing 4 to 8 times liquefied propane with respect to the vacuum distillation residual oil and extracting the degassed oil at an extraction temperature of 55 to 75 ° C. The solvent deasphalted asphalt removed in step S13 has a penetration of 3 to 20 (1/10 mm), a softening point of 56 to 70 ° C., and a density at 15 ° C. of 1020 to 1065 kg / m for the reasons described above. It should be ³ . Similarly, it is desirable that the kinematic viscosity at 100 ° C. of the solvent removal solvent is 25 to 42 mm ² / s and the density at 15 ° C. is 910 to 940 kg / m ³ . The separated solvent deasphalted asphalt is used in a mixing process to be described later, so it is stored as it is or stored in an intermediate tank or the like in the refinery. In addition, since the separated solvent-depleted oil is also used in the mixing process described later, a part is taken out and stored, but the rest is used for the processing shown in the next step S14. Become.

  In step S14, solvent extraction oil as an extract is obtained by solvent extraction of the solvent-depleted oil using a polar solvent. As the polar solvent used in step S14, for example, furfural, N-methyl-2-pyrrolidone (NMP), phenol, cresolic acid, sulfur disulfide, nitrobenzene, aniline and the like are used. In this step S14, the volume ratio of the polar solvent to be mixed with the solvent deasphalted oil is in the range of 2 to 4, and preferably in the range of 2.5 to 3.5. The extraction temperature in step S14 is preferably 40 to 140 ° C. The solvent extracted oil finally obtained in step S14 is stored for use in the mixing process described later.

  Next, the process proceeds to step S15, and a desired aniline point and a desired kinematic viscosity in the process oil to be actually produced are selected. Incidentally, the aniline point and kinematic viscosity may be freely selected independently of each other, and when either one is selected, the other is not uniquely determined according to this. Next, the mixing ratio of solvent deasphalted asphalt, solvent deasphalted oil, and solvent extracted oil for adjusting to the selected aniline point and kinematic viscosity is determined.

FIG. 2 shows the relationship of the mixing ratio of solvent deasphalted asphalt, solvent deasphalted oil, and solvent extracted oil with respect to kinematic viscosity and aniline point, as clarified by the present inventors. According to FIG. 2, the horizontal axis indicates the kinematic viscosity (mm ² / s) at 100 ° C., and the vertical axis indicates the aniline point (° C.). The bold solid line indicates the kinematic viscosity with respect to the mixing ratio of the solvent deasphalted asphalt (PDA). , Shows the relationship of aniline points. By the way, this FIG. 2 shows that asphalt with solvent removal, the penetration at 25 ° C. is 8 (1/10 mm), the softening point is 66.5 ° C., and the density at 15 ° C. is 1028 kg / m ³ under JIS K2207. Yes, the kinematic viscosity at 100 ° C. for the solvent-depleted oil is 33.2 mm ² / s, the density at 15 ° C. is 926.2 kg / m ³ , and the kinematic viscosity at 100 ° C. is 65.0 mm ² / s for the solvent-extracted oil. The density at 15 ° C. is 976.4 kg / m ³ . By the way, even if the physical properties of solvent-deasphalted asphalt, solvent-desorbed oil, and solvent-extracted oil deviate from the above-mentioned values, although the slope of the curve and the interval between adjacent curves are different from those in FIG. Of course, a similar curve can be drawn, and the method described below can be similarly realized.

  By way of example, the solvent-developed asphalt shows 1.0, 2.5, 5, 10, 15, 20% by weight. A comparative example with a PDA of 25% is also shown. The bold solid line shows that the relationship between the kinematic viscosity and the aniline point changes in a curved line from the upper left to the lower right. It is also shown that the slope of the curve tends to become gentler as the mixing ratio of the solvent-desorbed asphalt increases.

  According to the present invention, the solvent-deasphalted asphalt may contain 1.0 to 20% by weight as an essential requirement. The reason for this is that if the solvent-free asphalt is less than 1.0% by weight, it becomes difficult to adjust the kinematic viscosity especially when assuming tire use, and if the solvent-deleted asphalt exceeds 20% by weight, This is because the kinematic viscosity becomes high and the rubber itself becomes too hard as shown in the example of PDA 25% in FIG. Further, when the asphalt desorbed from the solvent exceeds 20% by weight, the adjustment range of the aniline point becomes narrow, which is not practical.

  Moreover, the dotted line in a figure has shown the relationship of kinematic viscosity and the aniline point with respect to the mixing ratio of solvent debris oil and solvent extraction oil. The mixing ratio of solvent-depleted oil and solvent-extracted oil indicates the weight ratio of solvent-desorbed oil and solvent-extracted oil that constitutes the residue after subtracting the above-mentioned weight% of solvent-desorbed asphalt from the entire process oil. . For example, the solvent removal oil (DAO) and the solvent extraction oil (BFE) are DAO: BFE = 100: 0, 75:25, 50:50, 25:75, 0: 100, respectively. Is shown. The dotted lines show that the relationship between the kinematic viscosity and the aniline point changes in a curved line from the upper left to the lower right. In addition, as the mixing ratio of the solvent extraction oil (BFE) increases, the slope of the curve gradually becomes gentle. Especially when DAO: BFE = 0: 100, the aniline point becomes almost constant at 67 ° C. , It tends to be indicated by a horizontal line rather than a curve.

  It is noted that the bold solid line corresponding to the mixing ratio of solvent deasphalted asphalt (PDA) tends to be more inclined than the dotted line corresponding to the weight ratio of solvent deasphalted oil and solvent extracted oil.

  In the present invention, the selected desired aniline point and desired kinematic viscosity are compared with the tendency shown in FIG. 2 to determine the mixing ratio of solvent-deasphalted asphalt, solvent-desorbed oil, and solvent-extracted oil.

For example, when the kinematic viscosity is 69 mm ² / s and the aniline point is selected to be 76 ° C., the corresponding point on FIG. In this point A, the mixing ratio of solvent deasphalted asphalt (PDA) is 10% by weight. The remaining 90% by weight is composed of solvent removal oil (DAO) and solvent extraction oil (BFE), but at point A, DAO: BFE is exactly 25:75. For this reason, the solvent deasphalting asphalt, the solvent deasphalting oil, and the solvent extraction oil are mixed in this way and selected in step S16 of FIG. 1 by mixing them based on the determined mixing ratio. A process oil having a kinematic viscosity of 69 mm ² / s and an aniline point of 76 ° C. can be produced. For example, when the kinematic viscosity is selected to be 58 mm ² / s and the aniline point is 82 ° C., the corresponding point on FIG. As for this B point, the mixing ratio of solvent deasphalted asphalt (PDA) is 7.5% by weight. The remaining 92.5% by weight is composed of solvent removing oil (DAO) and solvent extracted oil (BFE), but at point B, DAO: BFE is just 37.5: 62.5. For this reason, the solvent deasphalting asphalt, the solvent deasphalting oil, and the solvent extraction oil are mixed in this way and selected in step S16 of FIG. 1 by mixing them based on the determined mixing ratio. A B-point process oil having a kinematic viscosity of 58 mm ² / s and an aniline point of 82 ° C. can be produced.

  Actually, a method for obtaining the mixing ratio of the point B will be described in detail with reference to FIG. First, a line is drawn horizontally and vertically around point B. As a result, the vertical line intersects the curve with DAO: BFE of 50:50 and DAO: BFE with the curve of 25:75. Similarly, the horizontal line from point B intersects the curve of PDA 5% and the curve of PDA 10%.

Next, the distance between the intersection point with these curves and point B is obtained from the figure. B point and the DAO: BFE _x 1 the distance between the curve of 50:50, B point and the DAO: BFE is a distance between the curve of 25:75 and _{x 2.} Further, the distance between the point B and the PDA 5% curve is y ₁ , and the distance between the point B and the PDA 10% curve is y ₂ . At this time, the ratio of DAO in DAO: BFE at point B can be obtained by the following calculation formula.

DAO ratio = DAO (lower side) ratio + x ₂ / (x ₁ + x ₂ ) × {DAO (upper side) ratio−DAO (lower side) ratio}

Here, the upper side corresponds to a DAO: BFE curve located above the point B, and the ratio of DAO (upper side) in this example is 50. The lower side corresponds to a DAO: BFE curve located below the point B, and the DAO (lower side) ratio in this example is 25. Further, _{x 1} and _{x 2} are the line segment ratio is 1: Since a _1, since the x 2 _{/ (x} 1 + _{x 2)} The sections 0.5, the ratio of the DAO is 25 + 0.5 × ( 50−25) = 37.5, and the ratio of BFE is also 62.5.

  Further, the PDA ratio at point B can be obtained by the following calculation formula.

PDA ratio = PDA (left side) ratio + y ₁ / (y ₁ + y ₂ ) × {PDA (right side) ratio−PDA (left side) ratio}

Here, the left side corresponds to a PDA 5% curve located on the left side of point B. The right side corresponds to a curve of 10% PDA located on the right side of point B. Moreover, since the line segment ratio of y ₁ and y ₂ was 1: 1, the term y ₁ / (y ₁ + y ₂ ) is 0.5, so the PDA ratio is 5 + 0.5 × ( 10−5) = 7.5. Thus, according to the present invention, in the graph consisting of two axes of kinematic viscosity and aniline, the first curve (PDA curve) showing the relationship between the aniline point and kinematic viscosity for each mixing ratio of the asphalt investigated in advance, and The second curve (DAO: BFE curve) showing the relationship between the aniline point and the kinematic viscosity with respect to the solvent degreasing oil and the mixing ratio of the solvent degreasing oil investigated in advance is entered, and the desired aniline point and kinematic viscosity are the first. When corresponding to the intersection of the curve and the second curve, the mixing ratio is obtained from the first curve and the second curve passing through the intersection. Further, when the desired aniline point and kinematic viscosity are located other than the intersection of the first curve and the second curve, a vertical line and a horizontal line are drawn from the desired aniline point and the desired point B on the graph corresponding to the kinematic viscosity. Pull. Then, the mixing ratio of asphalt is obtained based on the distance ratio between the intersections b ₁ and b ₂ with the first two curves where the horizontal line first intersects with the desired point B, and the two second curves where the vertical line first intersects. Based on the distance ratio between the intersection points a ₁ and a ₂ and the desired point B, the mixing ratio of the solvent-depleted oil and the solvent-extracted oil is determined.

  This makes it possible to easily determine the mixing ratio even when the desired aniline point and kinematic viscosity are located outside the intersection of the first curve and the second curve.

  Similarly, even for other combinations of kinematic viscosity and aniline point, the corresponding point on FIG. 2 is identified, the mixing ratio of the solvent-deasphalted asphalt corresponding to this is identified, and then the solvent-desorbed oil By specifying the mixing ratio of the solvent extraction oil, it becomes possible to produce a process oil having the selected kinematic viscosity and aniline point.

  In the present invention, even when the combination of the selected kinematic viscosity and the aniline point deviates from the intersection of the bold solid line and the dotted line described above, the intersection of the desired dynamic viscosity and the DAO: BFE curve of the vertical line from the aniline point. The ratio of DAO: BFE and PDA can be easily obtained based on the above formula from the distance ratio from the distance from the intersection of the desired kinematic viscosity and the PDA ratio of the horizontal line from the aniline point. Is possible. Then, by determining the mixing ratio of solvent-deasphalted asphalt, solvent-desorbed oil, and solvent-extracted oil, it becomes possible to produce a process oil having a desired kinematic viscosity and aniline point.

  In addition, even when these solvent deasphalted asphalt, solvent deasphalted oil, and solvent extracted oil deviate from the above-mentioned physical property range, although the tendency of each curve shown in FIG. The general trend is almost unchanged. That is, the change in the physical properties of the solvent deasphalting asphalt affects the change in the shape of the right side portion (PDA 20% line) of the region shown in FIG. 2, and the change in the physical properties of the solvent deasphalting oil is shown in FIG. 2 affects the change in the shape of the upper side portion (DAO: BFE = 100: 0 line) of the region to be changed, and the change in the physical properties of the solvent-extracted oil is caused by the lower side portion (DAO: BFE = 0) of the region shown in FIG. : 100 lines). However, even if the shape of these curves changes, a desired aniline point and a desired kinematic viscosity are selected and created by preparing a relationship diagram as shown in FIG. 2 for each physical property. The mixing ratio of solvent deasphalted asphalt, solvent deasphalted oil, and solvent extracted oil is determined by comparing with the relationship diagram. Needless to say, the mixing ratios at that time are limited to those having the physical properties of solvent-deasphalted asphalt, solvent-depleted oil, and solvent-extracted oil used in creating the relationship diagram.

  In the above-described example, the solvent-deasphalted asphalt is mainly described with respect to a so-called three-component system in which solvent-depleted oil and solvent-extracted oil are mixed. However, the present invention is not limited to this. Of course, it may be constituted by a so-called two-component system as in the case of mixing solvent-depleted oil with deasphalted asphalt, or when mixing solvent-extracted oil with desolvated asphalt. In such a case, the adjustment of components in the DAO: BFE = 100: 0 line and the DAO: BFE = 0: 100 line in FIG.

  Further, in the present invention, any asphalt such as blown asphalt and straight asphalt may be used as an alternative to solvent deasphalted asphalt, but in such a case, the slope of the curve and the interval between adjacent curves are different from those in FIG. Although it is different, it is possible to draw a curve similar to that of solvent-free asphalt. For this reason, even when applying such asphalt, the kinematic viscosity and the aniline point graph are created in advance in the relationship with the solvent removal oil and the solvent extraction oil, so that the kinematic viscosity is similar to the above-described example. The process oil can be produced with low labor and low cost by freely selecting a combination of the aniline point and the aniline point.

It is a flowchart which shows the manufacturing method of the process oil to which this invention is applied. It is a figure which shows the relationship of the mixing ratio of solvent deasphalting asphalt, solvent deasphalting oil, and solvent extraction oil with respect to kinematic viscosity and an aniline point. It is a figure for demonstrating the method of actually calculating | requiring the mixing ratio of B point.

Explanation of symbols

S11 Atmospheric distillation S12 Vacuum distillation S13 Solvent removal S14 Solvent extraction S15 Specification of desired property S16 Mixing

Claims (5)

Against asphalt, only the solvent extracted oil obtained by the obtained solvent deasphalted oil及beauty above Symbol solvent deasphalted oil obtained by solvent deasphalting the vacuum residue oil in oil solvent extraction is desired aniline point and Process oil characterized by being mixed so as to have a desired kinematic viscosity. The process oil according to claim 1, wherein the asphalt is a solvent deasphalted asphalt obtained by desolvating the vacuum distillation residue of crude oil. The solvent deasphalted asphalt, 1.0 to 20 is contained by weight%, the process oil according to claim 2, wherein the balance being composed of the solvent deasphalted oil及beauty above Symbol solvent extracted oil. The process oil according to claim 1, wherein the aniline point is 75 to 90 ° C. and the kinematic viscosity is 40 to 90 mm ² / s. A rubber extension oil comprising the process oil according to any one of claims 1 to 3.